CN109851697A - A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process - Google Patents
A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process Download PDFInfo
- Publication number
- CN109851697A CN109851697A CN201910114200.2A CN201910114200A CN109851697A CN 109851697 A CN109851697 A CN 109851697A CN 201910114200 A CN201910114200 A CN 201910114200A CN 109851697 A CN109851697 A CN 109851697A
- Authority
- CN
- China
- Prior art keywords
- solvent
- stripping
- oligomer
- desolventizing
- low pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of commercial runs for removing solvent and oligomer suitable for hydrogenated petroleum resin production process.The process of this method description is composed in series by low pressure desolventizing unit and using the dissolved hydrogen of hydrogenation process discharge or discharge hydrogen as the stripping desolventizing and oligomer units of stripping fluid, material enters back into stripping desolventizing and oligomer units removing oligomer and remaining solvent after low pressure desolventizing unit removes most of solvent or almost all solvent, to realize the removing of solvent and oligomer in Petropols solution.This method using dissolved hydrogen, discharge hydrogen or the low molecule fixed gas for containing equilibrium composition solvent identical with system solvent ingredient due to, as stripping fluid, having been maximally reduced solvent loss, having reduced material consumption.Simultaneously because using equipment such as falling film evaporators, have the characteristics that high-efficient, solvent loss is small, low energy consumption without waste water and process.
Description
Technical field
The present invention relates to a kind of commercial runs for removing solvent and oligomer suitable for hydrogenated petroleum resin production process.
The process of this method description is made of low pressure removing process and stripping desolventizing and oligomer process, low pressure desolventizing unit master
Solvent is removed, the material for removing most of solvent or almost all solvent enters back into stripping desolventizing and oligomer units removing
Oligomer and remaining solvent, to realize the removing of solvent and oligomer in Petropols solution.Wherein stripping fluid is to add
The discharge hydrogen of the steam containing solvent of hydrogen process low-pressure gas-liquid separator discharge or the steam containing solvent of low pressure removing process discharge
Dissolved hydrogen, be also possible to the low molecule fixed gas of extraneous input；This method stone suitable for hydrogenated petroleum resin production process
The removing of contained solvent and oligomer, it is molten to be also applied for other polymers in oleoresin polymeric solution and hydrogenation of petroleum resin product
The removing of solvent and oligomer in liquid；Method disclosed by the invention is serious to temperature and residence time especially suitable for product quality
Sensitive object system has the characteristics that high-efficient, solvent loss is small, low energy consumption without waste water and process.
Background technique
The production process of hydrogenated petroleum resin includes Petropols polymerization and two main process of hydrogenation of petroleum resin, as being permitted
The production process of heteropolymer is the same, needs to use a large amount of solvents, and due to the drop in polymerization process and hydrogenation process
Solution reaction inevitably generates oligomer, average molecular weight of the residual quantity of solvent and oligomer to product, dispersion in product
The indexs such as degree, softening point, rheological property have significant impact, and the removal methods or process of solvent and oligomer influence residual quantity
It is huge.
It is industrial universal in order to remove the solvent and oligomer in Petropols polymeric solution and hydrogenation of petroleum resin product
Using atmospheric flashing or rectifying, and the method for combining stripping falling film evaporation or stripping rectifying, wherein stripping fluid largely uses water
The disadvantages of method of steam stripping, it is high that there are energy consumptions, and there are contaminated wastewaters.Especially during hydrogenation of petroleum resin, there is also
Product index such as coloration, bromine valency are to temperature and residence time serious tender subject.And the desolventizing mistake of Petroleum Resin Hydrogenation Process
Cheng Zhong is discharged a large amount of dissolved hydrogen and is not fully used, using this patent method, is situated between using dissolved hydrogen as stripping
Matter carries out the removing of solvent and oligomer, does not increase solvent consumption, while compared with steam stripping method, further decreasing
Energy consumption, solves the problems, such as discharge of wastewater, has the characteristics that high-efficient, solvent loss is small, low energy consumption without waste water and process.
Summary of the invention
The object of the present invention is to provide a kind of removing solvents suitable for hydrogenated petroleum resin production process and oligomeric
The commercial run of object；Technical scheme is as follows:
A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process, this method description
Process by low pressure desolventizing unit and using hydrogenation process discharge dissolved hydrogen or discharge hydrogen as the stripping desolventizing of stripping fluid
It is composed in series with oligomer units, material enters back into after low pressure desolventizing unit removes most of solvent or almost all solvent
Desolventizing and oligomer units removing oligomer and remaining solvent are stripped, to realize in Petropols solution solvent and oligomeric
The removing of object.
Low pressure desolventizing unit operating pressure is 0~0.3MPaG, strip desolventizing and oligomer units operating pressure be-
0.1~0MPaG；Operation pressure difference is 0.05~0.4MPa between low pressure desolventizing unit and stripping desolventizing and oligomer units, is taken
The delivery pump to disappear between unit for material conveying.
Low pressure desolventizing unit uses the list of equipment to be separated based on rectifying column, flash tank or falling film evaporator with single-stage
Grade desolventizing scheme, removes major part or almost all solvent, stripping fluid of the dissolved hydrogen of discharge as stripping process；Removing
The material of major part or almost all solvent enters back into stripping desolventizing and oligomer units removing oligomer and remaining solvent；
Suitable for the process it is not necessary that solvent to be separated into two or more solvent by boiling range or composition.
Low pressure desolventizing unit uses the equipment to be separated based on rectifying column, flash tank or falling film evaporator, and by wantonly two
Kind combination of the above and the two-stage being connected in series or multistage desolventizing scheme, are successively separated into two kinds or two by boiling point, boiling range or composition
Kind or more solvent, while removing major part or almost all solvent, the dissolved hydrogen of discharges at different levels is incorporated as the vapour of stripping process
Recommend matter；Removing major part or almost all solvent material enter back into stripping desolventizing and oligomer units removing oligomer and
Remaining solvent；It is applicable to for solvent to be separated into the process of two or more solvent by boiling point, boiling range or composition.
The falling film evaporator of the preferred counter-current operation of single-stage desolventizing scheme；Level-one desolvating device in two-stage desolventizing scheme
It is preferred that using rectifying column or flash tank, second level desolvating device preferably uses the falling film evaporator of counter-current operation.
The process of the stripping desolventizing and oligomer is stripping fluid for hydrogenation process low-pressure gas-liquid separator row
The dissolved hydrogen of the steam containing solvent of discharge hydrogen or low pressure the removing process discharge of the steam containing solvent out.
The process of stripping desolventizing and oligomer is the combination using gas compressor or vacuum pump and gas compressor
The circulation of stripping fluid is realized, to meet the minimum of requirement and exhaust emissions to stripping fluid flow.
The process of stripping removing solvent and oligomer is to steam using the falling film evaporator or stripping of countercurrent or cocurrent operation
Evaporate tower, the preferably falling film evaporator of counter-current operation.
Different stream is selected according to different treating material features and processing requirement using the process that this method describes
Journey configuration, can complete the separation task of removing solvent and oligomer；Since the fixed gas using low molecular weight is situated between as stripping
Matter greatly reduces plant energy consumption, and process non-wastewater discharge；Due to using dissolved hydrogen, discharge hydrogen or containing molten with system
The low molecule fixed gas of the identical equilibrium composition solvent of agent ingredient has maximally reduced solvent loss as stripping fluid,
Reduce material consumption.Simultaneously because this method is especially suitable for product quality to temperature and stop using equipment such as falling film evaporators
Time serious sensitive object system has the characteristics that high-efficient, solvent loss is small, low energy consumption without waste water and process.
Detailed description of the invention
Fig. 1: hydrogenated petroleum resin production process desolventizing and oligomer process flow diagram (single-stage low pressure desolventizing side
Case)；
Fig. 2: (two-stage or multistage low pressure are de- for hydrogenated petroleum resin production process desolventizing and oligomer process flow diagram
Solvent scheme)；1 heater, 2 level-one low pressure separator (rectifying column, flash tank or falling film evaporator), 3 level-one low-pressure condenser
4 second level low pressure separators (rectifying column, flash tank or falling film evaporator), 5 second level low-pressure condenser 6 strips separator (stripping drop
Film evaporator or stripping destilling tower) 7 stripping stripping gas-liquid separator (gas-liquid separator or the oligomer knockout towers) 9 of condensers 8
11 low-temperature condenser of stripping gas exhaust pump (vacuum pump or gas compressor) 10 circulating air gas-liquid separator, 12 stripping gas circulation
Pump circulation stripping 14 stripping fluid heater of hot-air heater, the 15 level-one low-pressure gas-liquid point of (circulating fan or gas compressor) 13
From device (return tank or gas-liquid separator).
Specific embodiment
Following instance further illustrates the feature and details of this technique, but listed process and data are not meant to this hair
The limitation of bright range.Entire technical process is by low pressure removing process and stripping desolventizing and the two unit series connection of oligomer process
Composition, low pressure desolventizing unit mainly remove solvent, and the material for removing most of solvent or almost all solvent enters back into stripping
Desolventizing and oligomer units removing oligomer and remaining solvent, to realize solvent and oligomer in Petropols solution
Removing；Operation pressure difference is 0.05~0.4MPa between low pressure desolventizing unit and stripping desolventizing and oligomer units, can be cancelled
Delivery pump between unit for material conveying, operating pressure and pressure difference meet to be wanted without fluid delivery pump downstream transport material
It asks.This method is not only applicable in hydrogenated petroleum resin production process in Petropols polymeric solution and hydrogenation of petroleum resin product
The removing of contained solvent and oligomer is also applied for the removing of solvent and oligomer in other polymers solution.
It is separation of oligomeric for stripping desolventizing and oligomer process, main purpose, can be grasped using countercurrent or cocurrent
The falling film evaporation of work or stripping distillation process, the preferably falling film evaporator of counter-current operation, generally operate under normal or reduced pressure, grasp
Make Minimum Technological Requirement of the pressure depending on upstream material the conveying differential pressure requirements for coming required and de- oligomer effect, operation pressure
Power range is -0.1~0MPaG；The process stripping fluid is the steam containing solvent of hydrogenation process low-pressure gas-liquid separator discharge
The dissolved hydrogen of the steam containing solvent of hydrogen or the discharge of low pressure removing process is discharged, the low molecule for being also possible to extraneous input does not coagulate
Gas, and containing identical with system solvent ingredient equilibrium composition solvent, including hydrogen, nitrogen, ethane, propane etc., preferably dissolve
Hydrogen；Meanwhile the process realizes the circulation of stripping fluid using the combination of gas compressor or vacuum pump and gas compressor, with full
The minimum of requirement and exhaust emissions of the foot to stripping fluid flow.Since the fixed gas using low molecular weight is situated between as stripping
Matter, the dissolved hydrogen being unavoidably discharged in particular by hydrogenation process and discharge hydrogen, strip ratio with using water vapour, have efficiency
It is higher, solvent loss is smaller, without waste water and the lower feature of process energy consumption, especially suitable for product quality to temperature and when stopping
Between serious sensitive object system, such as the removing of the desolventizing and oligomer of Petropols.
For low pressure removing process, mainly for separating of solvent, generally it is in low pressure or normal pressing operation, operating pressure
0~0.3MPaG；The process is divided into single-stage desolventizing and two-stage or two sides of multistage desolventizing according to the difference of solvent separation requirement
Case.
Single-stage desolventizing scheme is relatively narrow suitable for solvent boiling range, it is not necessary that solvent is separated into two kinds or two by boiling range or composition
Kind or more solvent process, for removing major part or almost all solvent, stripping of the dissolved hydrogen of discharge as stripping process
Medium；The material for removing most of solvent or almost all solvent enters back into stripping desolventizing and oligomer units removing oligomer
With remaining solvent, to realize the removing of solvent and oligomer in Petropols solution.The program with rectifying column, flash tank or
Equipment to be separated based on falling film evaporator (countercurrent or cocurrent), the preferably falling film evaporator of counter-current operation.
The protocol procedures schematic diagram of single-stage desolventizing is as shown in Fig. 1: from hydrogenation of petroleum resin device low pressure separator or
The heated device 1 of the Petropols solution containing solvent and oligomer of polyplant discharge is heated to set temperature, into low pressure point
Vapor-liquid separation is carried out from device (rectifying column, flash tank or falling film evaporator) 4；Solvent steam enters after the condensation of low-pressure condenser 5
Circulating air gas-liquid separator 10；The Petropols solution of most of solvent is removed under the promotion of enough equipment pressure differences or delivery pump
Into stripping separator (stripping falling film evaporator or stripping destilling tower) 6, material stripping separator (stripping falling film evaporator or
Stripping destilling tower) solvent, oligomer are separated with Petropols under the action of stripping fluid in 6；Petropols are separated from stripping
Device (stripping falling film evaporator or stripping destilling tower) 6 bottoms are discharged into next technical process such as granulating and forming process；It is solvent, low
Polymers steam is cooled to set temperature by stripping condenser 7 and enters stripping gas-liquid separator (gas-liquid separator or oligomer point
From tower) 8, it is condensed out in this process oligomer, and separated with uncooled solvent and stripping fluid；Oligomer is by stripping gas-liquid
The discharge of separator (gas-liquid separator or oligomer knockout tower) 8 bottoms, vapour phase (uncooled solvent and stripping fluid) is through stripping
Gas exhaust pump (vacuum pump or compressor) 9 is discharged into circulating air gas-liquid separator 10；Into the gas-liquid of circulating air gas-liquid separator 10
Mixture is divided into gas-liquid two-phase wherein, and liquid phase solvent is discharged from bottom, and vapour phase is mainly the vapour phase solvent of dissolved hydrogen and balance；
When circulating air gas-liquid separator 10 is that low pressure operates, a part of vapour phase is discharged through low-temperature condenser 11, and condensate liquid returns
Circulating air gas-liquid separator 10, and maintaining circulating air gas-liquid separator 10 is the pressure of setting；Remaining vapour phase is by the flow set
Enter stripping separator (stripping falling film evaporator or stripping destilling tower) 6 as stripping fluid through circulation stripping hot-air heater 13；
When circulating air gas-liquid separator 10 is atmospheric operation, vapour phase is pressurized by stripping gas circulating pump (circulating fan or compressor) 12,
A part is discharged through low-temperature condenser 11, and condensate liquid returns to circulating air gas-liquid separator 10, and maintains stripping gas circulating pump (circulation
Blower or compressor) 12 outlet pressures；Remaining vapour phase is used as stripping fluid through circulation stripping hot-air heater 13 by the flow of setting
Into stripping separator (stripping falling film evaporator or stripping destilling tower) 6.When in feed polymer solution be free of dissolved hydrogen when or
When dissolved hydrogen underfed, stripping fluid can not be coagulated using the low boiling point of the discharge hydrogen for adding hydrogen low pressure separator or extraneous input
Gas enters stripping separator (stripping falling film evaporator or stripping destilling tower) as stripping fluid through circulation stripping hot-air heater 13
6。
Two-stage or multistage desolventizing scheme are wider suitable for solvent boiling range, need solvent by boiling point, boiling range or group ingredient
From the process for two or more solvent, it is molten two or more successively can be separated by boiling point, boiling range or composition
Agent, removes major part or almost all solvent, the dissolved hydrogen of discharges at different levels are incorporated as the stripping fluid of stripping process；Removing is big
The material of partial solvent or almost all solvent enters back into stripping desolventizing and oligomer units removing oligomer and remaining molten
Agent, to realize the removing of solvent and oligomer in Petropols solution.The every level-one of the program is with rectifying column, flash tank or drop
Equipment to be separated based on film evaporator, and be connected in series and be composed by two or more equipment；For two-stage desolventizing scheme, level-one
Desolvating device preferably uses rectifying column or flash tank, and second level desolvating device preferably uses the falling film evaporator of counter-current operation.
The protocol procedures schematic diagram of two-stage desolventizing is as shown in Fig. 2: from hydrogenation of petroleum resin device low pressure separator or
The Petropols solution containing solvent and oligomer of polyplant discharge or other passed through containing the polymer solution of solvent and oligomer
Heater 1 is heated to set temperature, into level-one low pressure separator (rectifying column, flash tank or falling film evaporator) 2, in setting temperature
It spends lower low boiling point solvent to separate with Petropols, vapour phase enters the (reflux of level-one low-pressure gas-liquid separator through level-one low-pressure condenser 3
Tank or gas-liquid separator) 15 and it is divided into vehicle repair major, liquid phase is produced as low boiling point solvent, and vapour phase is through stripping fluid heater 14
Enter stripping separator (stripping falling film evaporator or stripping destilling tower) 6 as stripping fluid.Level-one low pressure separator (rectifying
Tower, flash tank or falling film evaporator) liquid phases of 2 discharges be the Petropols solution of removing low boiling point solvent, in enough pressure differences or
Enter second level low pressure separator (rectifying column, flash tank or falling film evaporator) 4 under the promotion of product pump, in higher set temperature
Lower high boiling solvent is separated with Petropols, enters circulating air gas-liquid separator 10 after the condensation of second level low-pressure condenser 5；Second level
The Petropols for the removing high boiling solvent that low pressure separator (rectifying column, flash tank or falling film evaporator) 4 is discharged are being set enough
Enter stripping separator (stripping falling film evaporator or stripping destilling tower) 6, work of the material in stripping fluid under the promotion of standby pressure difference
It is divided into gas-liquid two-phase under；Liquid phase melt from stripping separator (stripping falling film evaporator or stripping destilling tower) 6 bottoms be discharged into
Enter next technical process such as granulating and forming process；Vapour phase is cooled to set temperature by stripping condenser 7 and enters stripping gas-liquid point
From device (gas-liquid separator or oligomer knockout tower) 8, condensed out in this process oligomer, and with uncooled solvent and stripping
Medium separation；Oligomer is discharged by stripping gas-liquid separator (gas-liquid separator or oligomer knockout tower) 8 bottoms, and vapour phase is not (cold
Solidifying solvent and stripping fluid) through stripping gas exhaust pump (vacuum pump or compressor) 9 it is discharged into circulating air gas-liquid separator 10；Into
The gas-liquid mixture of circulating air gas-liquid separator 10 is divided into gas-liquid two-phase wherein, and liquid phase is that high boiling solvent is discharged from bottom,
Vapour phase is mainly the vapour phase solvent of dissolved hydrogen and balance；When circulating air gas-liquid separator 10 is that low pressure operates, the one of vapour phase
Part is discharged through low-temperature condenser 11, and condensate liquid returns to circulating air gas-liquid separator 10, and maintains circulating air gas-liquid separator 10
For the pressure of setting；Remaining vapour phase enters stripping separation as stripping fluid through circulation stripping hot-air heater 13 by the flow of setting
Device (stripping falling film evaporator or stripping destilling tower) 6；When circulating air gas-liquid separator 10 is atmospheric operation, vapour phase is by stripping gas
Circulating pump (circulating fan or compressor) 12 is pressurized, and a part is discharged through low-temperature condenser 11, and condensate liquid returns to circulating air gas-liquid
Separator 10, and maintain stripping gas circulating pump (circulating fan or compressor) 12 outlet pressures；Remaining vapour phase is by the flow set
Enter stripping separator (stripping falling film evaporator or stripping destilling tower) 6 as stripping fluid through circulation stripping hot-air heater 13.
When being free of dissolved hydrogen in feed polymer solution or when dissolved hydrogen underfed, stripping fluid can use plus the separation of hydrogen low pressure
The discharge hydrogen of device or the low boiling point fixed gas of extraneous input enter stripping point as stripping fluid through circulation stripping hot-air heater 13
From device (stripping falling film evaporator or stripping destilling tower) 6.
Related table is device configuration and operating condition list in example.
Embodiment 1-2:(exemplary flow such as Fig. 1)
Embodiment 3-4:(exemplary flow such as Fig. 1)
Embodiment 5-6:(exemplary flow such as Fig. 2)
Embodiment 7-8:(exemplary flow such as Fig. 2)
Embodiment 9-10:(exemplary flow such as Fig. 2)
Embodiment 11-12:(exemplary flow such as Fig. 2)
From above example it can be concluded that using this method describe process, according to different treating materials
Feature and processing requirement select different processes to configure, and can complete the separation task of removing solvent and oligomer；Due to using
The fixed gas of low molecular weight greatly reduces plant energy consumption, and process non-wastewater discharge as stripping fluid；Due to using molten
Xie Qing, discharge hydrogen contain the low molecule fixed gas of equilibrium composition solvent identical with system solvent ingredient as stripping fluid,
Solvent loss has been maximally reduced, material consumption is reduced.Simultaneously because this method is especially suitable using equipment such as falling film evaporators
For product quality to temperature and residence time serious sensitive object system, with high-efficient, solvent loss is small, without waste water and process
The characteristics of low energy consumption.
Claims (8)
1. a kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process, this method description
Process by low pressure desolventizing unit and using the dissolved hydrogen of hydrogenation process discharge or discharge hydrogen as the stripping desolventizing of stripping fluid and
Oligomer units are composed in series, and material enters back into vapour after low pressure desolventizing unit removes most of solvent or almost all solvent
Desolventizing and oligomer units removing oligomer and remaining solvent are mentioned, to realize solvent and oligomer in Petropols solution
Removing.
2. commercial run as described in claim 1, it is characterized in that low pressure desolventizing unit operating pressure is 0~0.3MPaG, vapour
It mentions desolventizing and oligomer units operating pressure is -0.1~0MPaG；Low pressure desolventizing unit and stripping desolventizing and oligomer
It is 0.05~0.4MPa that pressure difference is operated between unit, cancels the delivery pump between unit for material conveying.
3. commercial run as described in claim 1, it is characterized in that low pressure desolventizing unit is used with the rectifying column of single-stage, flash distillation
The single-stage desolventizing scheme of equipment to be separated based on tank or falling film evaporator, removes major part or almost all solvent, discharge
Stripping fluid of the dissolved hydrogen as stripping process；Removing major part or almost all solvent material enter back into stripping desolventizing and
Oligomer units remove oligomer and remaining solvent；Suitable for it is not necessary that solvent is separated into two kinds or two kinds by boiling range or composition
The process of the above solvent.
4. commercial run as described in claim 1, it is characterized in that low pressure desolventizing unit is used with rectifying column, flash tank or drop
Equipment to be separated based on film evaporator, and by any two combination of the above and the two-stage being connected in series or multistage desolventizing scheme, successively
It is separated into two or more solvent by boiling point, boiling range or composition, while removing major part or almost all solvent, Ge Jipai
Dissolved hydrogen out is incorporated as the stripping fluid of stripping process；The material of removing major part or almost all solvent enters back into stripping
Desolventizing and oligomer units removing oligomer and remaining solvent；It is applicable to solvent by boiling point, boiling range or group ingredient
From the process for two or more solvent.
5. commercial run as described in claim 1, it is characterized in that the falling film evaporation of the preferred counter-current operation of single-stage desolventizing scheme
Device；Level-one desolvating device preferably uses rectifying column or flash tank in two-stage desolventizing scheme, and second level desolvating device is preferably adopted
With the falling film evaporator of counter-current operation.
6. commercial run as described in claim 1, it is characterized in that the process of the stripping desolventizing and oligomer is vapour
Recommend discharge hydrogen or the discharge of low pressure removing process of the steam containing solvent that matter is the discharge of hydrogenation process low-pressure gas-liquid separator
The dissolved hydrogen of the steam containing solvent.
7. commercial run as described in claim 1, it is characterized in that the process of stripping desolventizing and oligomer is using gas
The circulation of stripping fluid is realized in the combination of compressor or vacuum pump and gas compressor, to meet the requirement to stripping fluid flow
With the minimum of exhaust emissions.
8. commercial run as described in claim 1, it is characterized in that the process of stripping removing solvent and oligomer is using inverse
The falling film evaporator or stripping destilling tower of stream or cocurrent cooling operation, the preferably falling film evaporator of counter-current operation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910114200.2A CN109851697A (en) | 2019-02-13 | 2019-02-13 | A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910114200.2A CN109851697A (en) | 2019-02-13 | 2019-02-13 | A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN109851697A true CN109851697A (en) | 2019-06-07 |
Family
ID=66897799
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910114200.2A Pending CN109851697A (en) | 2019-02-13 | 2019-02-13 | A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109851697A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114230705A (en) * | 2021-12-15 | 2022-03-25 | 恒河材料科技股份有限公司 | Preparation method of flexible poly alpha-methylstyrene resin |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3442877A (en) * | 1965-07-20 | 1969-05-06 | Exxon Research Engineering Co | Two-stage hydrogenation process |
| CN102382259A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Industrial manufacture method for hydrogenated petroleum resin |
| CN103360547A (en) * | 2013-06-25 | 2013-10-23 | 朗盈科技（北京）有限公司 | System and method for producing dicyclopentadiene hydrogenated petroleum resin |
-
2019
- 2019-02-13 CN CN201910114200.2A patent/CN109851697A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3442877A (en) * | 1965-07-20 | 1969-05-06 | Exxon Research Engineering Co | Two-stage hydrogenation process |
| CN102382259A (en) * | 2010-08-30 | 2012-03-21 | 中国石油化工股份有限公司 | Industrial manufacture method for hydrogenated petroleum resin |
| CN103360547A (en) * | 2013-06-25 | 2013-10-23 | 朗盈科技（北京）有限公司 | System and method for producing dicyclopentadiene hydrogenated petroleum resin |
Non-Patent Citations (2)
| Title |
|---|
| 编写小组: "《石油炼制基本知识》", 30 September 1977, 石油工业出版社 * |
| 郑灌生等: "《润滑油生产装置技术问答》", 31 December 1998, 中国石化出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114230705A (en) * | 2021-12-15 | 2022-03-25 | 恒河材料科技股份有限公司 | Preparation method of flexible poly alpha-methylstyrene resin |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5227027A (en) | High efficiency water distillation apparatus using a heat pump system and process for use thereof | |
| RU2009119469A (en) | METHOD AND DEVICE FOR HYDROCARBON FLOW TREATMENT | |
| CN100512930C (en) | Process for the dehydration of gases | |
| CN102971057A (en) | Plant for recovering degraded heat transfer oil from a solar thermal facility and associated recovery method | |
| TWI630948B (en) | Method for concentrating water-soluble organic matter and device for concentrating water-soluble organic matter | |
| US6534619B1 (en) | Method for evaporating polymer solutions of thermoplastic polymers | |
| KR20220041122A (en) | Method for distilling a crude composition in a rectification plant comprising an indirect heat pump | |
| JP7468587B2 (en) | Method and apparatus for separating mixtures | |
| CN104185495B (en) | Process for recovering hydrocarbons from polyolefin plants and apparatus suitable for purpose | |
| EP3505542B1 (en) | Solvent separation apparatus and solvent separation method | |
| CN109851697A (en) | A kind of commercial run for removing solvent and oligomer suitable for hydrogenated petroleum resin production process | |
| CN1145003C (en) | Cryogenic rectification system for producing fuel and high-purity methane | |
| CN101384332A (en) | Reducing method of water from reactor outlet gas in the oxidation process of aromatic compound | |
| US3369344A (en) | Method for the recovery of deodorizer distillates | |
| CN1165805A (en) | Process of extracting phenols from phenol-containing waste water by means of solvent mixture | |
| CN1310857C (en) | Separation method of butenes and butanes by extractive distillation with a polar extractant | |
| US9486715B2 (en) | Process for purifying processing fluids | |
| KR102520447B1 (en) | Solvent recovery method and solvent recovery apparatus | |
| CZ299901B6 (en) | Cascade heating of distillation columns for separation of ethylbenzene and styrene and apparatus for making the same | |
| CN206940774U (en) | A kind of tetrahydrofuran dehydration device | |
| CN206300409U (en) | A kind of utilization associated gas isolates the processing unit of LPG and stable light hydrocarbon | |
| CN112694404B (en) | Method and device for purifying vinyl acetate in EVOH production process | |
| US20120272824A1 (en) | Method for drying natural gas by the joint cooling of solvent and natural gas | |
| CA2927028C (en) | Process for recovering heat from a hydrocarbon separation | |
| KR20170141875A (en) | Apparatus for separatiing solvent and method for recycling waste heat |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |